вход по аккаунту


Патент USA US2114352

код для вставки
April 19, 1938.
Al A. vM11-1:
Filed sept. 29, 1936
Patented Apr. 19, 1938
Arthur A. Neff, Paulsboro, N. J., assignor to `So-cony-Vacuum Oil Company, Incorporated, New
York, N. Y., a corporation of New York
Application September 29, 1936, Serial No. 103,066
2 Claims. (Cl. 196-1)
This invention is directed to the reiining of figure of which sets forth the process in diagram
oils, and particularly to the step of neutralizing matic form. In this drawing, the sour oil enters
high boiling point oils which have been acid through pipe I into mixing tank 2 which serves as
an accumulator for the system. From tank 2
High boiling point petroleum fractions, of the the oil is forced by pump 3 through heat ex 5
nature of lubricating oils, transformer oils, and changer 4, where it is heated to 30D/350° F. and
the like, are customarily refined by treatment then enters dry oil tank 5, which is equipped with
with sulphuric acid, for the precipitation of as
phaltic and color forming constituents, and the
10 like, resulting in the production of a sludge, which
is settled and Withdrawn, to be discarded, and a
so-called “sour” oil, which is neutralized and
further reñned for the production of ñnished
products. This invention has to do specifically
15 with this step of neutralization.
There are two general methods of neutraliza
tion practiced at present. The older method is
by treatment with aqueous solutions of caustic
soda. This may be, and usually is, preceded by
2 O a “gas blow”, in which the sour oil is thoroughly
blown and agitated with air to remove, in so far
as possible, all dissolved sulphur dioxide, and
other oxides of sulphur which may be displaced
during blowing. The sour oil at the end of the
25 “gas blow” is still high in acidity, and is then
neutralized bytreatment with aqueous caustic
soda. This operation is discontinuous, time con
suming, and frequently encounters difliculties
with emulsions, loss of oil color, and other trou
30 bles. A more modern method is one in which the
sour oil is admixed with a small amount of al
kaline absorbent clay, such as about 3-5% of
fuller’s earth and the like, heated moderately,
subjected to a “gas blow” operation at tempera
35 tures ranging from 200° F. to about 350° F., and
the mixed slurry of oil and clay then heated to
about 700° F., after which it is cooled and the oil
and clay separated by filtration. This process
a bottom steam spray 6 and a vent 1, in which is
mounted a steam jet 8 to provide a moderate
vacuum in tank 5. The hot oil is steamed thor 10
oughly in tank 5, under the vacuum existing
therein, and is then withdrawn by pump 9 and
passed through heat exchanger I0, being heated
to about 400° F. and then passes through line Il
and furnace heater I 2, where it is heated to a 15
temperature of G50/700° F. It is then discharged
into foam tank I3, equipped with steam spray I4
and vent I5, where gases formed during the sec
ond heating are expelled. The oil is then forced
by pump I6 through pipe I1, heat exchangers I0 20
and 4, and pipe I8 into blending tank I9, where it
is mixed with naphtha entering through pipe 20
in suflicient quantity to very materially reduce
its viscosity. The solution from the blending tank
is then strained to remove adventitious solid mat 25
ter and secure desired finish color by being forced
by pump 2| through blotter press 22, after which
it passes through percolation filter 23, (charged
with absorbent clay), and is removed from the
process as finished oil.
With this process, with
out the use of caustic and without contacting the
sour oil with clay, it is quite possible to secure
the same freedom from acidity as with former
procedure. The blotter press and percolator,
formerly charged with the duty of removing about 35
5% of fine clay from the oil, and constantly in
diiiiculty, now only clarify the oil solution, and
uses fine clay, and requires the use of filter
remain on stream great periods of time without
attention. Cost of clay consumed is completely
40 presses, thickeners, extractors, and the like for
removal and recovery of the clay. Not only is
there an added expense for clay purchase, but
the operative steps of clay removal are frequently
This capability of the process arises from its
feature of heating in two stages, each followed
in trouble, and give rise to high operative and
45 maintenance expense.
The object of this invention is to provide a
quick and eiiicient method for continuous neu
tralization of sour oil which does not make use
of admixed absorbent nor of caustic solutions.
This invention is based upon the discovery that
complete neutralization may be attained by the
application of heat and proper agitation with
inert gas.
In order to more completely under
stand this invention, reference is made to the
55 drawing attached to this specification, the single
avoided, and operating attendance is greatly 40
by thorough agitation and sweeping with inert
gas to remove the acidic constituents so set free. 45
In place of the steam, any inert gas, such as CO2,
and the like may be used, although steam is to be
preferred. The process may be carried out in
other apparatus setups which will suggest them
selves to the man skilled in the art as equivalents 50
of that which is herein disclosed by way of ex
ample only and not for the purpose of limiting
the disclosure thereby.
I claim:
1. A process for completely neutralizing “sour” 55
acid-treated high-boiling petroleum fractions
of from 300° to 350° F. in the absence of alkaline,
Without the use of adsorptive, agglomerative, or
adsorptive, or agglomerative material, thorough
alkaline materials comprising the following steps:
1y steaming the oil so heated under a subatmos
heating the oil to a temperature of from 300° to
350° F., and thoroughly agitating With inert gas
while subjecting the oil to subatmospheric pres
sure, thereafter further heating the oil to a. tem
perature of from 650° to '700° F., and further
thoroughly agitating with an inert gas.
2. A process for finishing “sour” acid-treated
high-boiling petroleum fractions comprising the
following steps; heating the oil toa temperature
pheric pressure, thereafter further heating ’the
oil in the absence of alkaline, adsorptive, or ag 5
glomerative material to a temperature of from
650° to 750° F., thoroughly steaming the oil so
heated, cooling the oil, adding thereto a Viscosity
reducing diluent, subjecting diluted oil to a slight
straining ñltration, and removing diluent.
Без категории
Размер файла
212 Кб
Пожаловаться на содержимое документа